Continuous process for the separation of mixtures of fatty substances of different melting points

ABSTRACT

The invention relates to an improvement of the known continuous process for the separation of mixtures of fatty substances of different melting points, in which the starting mixture by treating with an aqueous wetting agent solution is converted to a dispersion of liquid fatty substances and solid fatty substance particles, the formed dispersion is separated into two phases of different specific gravities, the lighter phase consists substantially of the liquid fatty fraction and the heavier phase of a dispersion of the solid fatty particles in the aqueous wetting agent solution. After separation of this suspension the wetting agent solution is returned to the process. The improvement consists in withdrawing a part of the recycling wetting agent solution from said dispersion of fatty particles in the aqueous wetting agent solution by separation of some or all the aqueous solution from the solid fatty particles, the solid fatty particles containing adhering aqueous phase and wetting agent are melted in the presence of an aqueous phase and the molten fatty fraction containing little wetting agent, is separated from the aqueous phase enriched with wetting agent which is recycled and the amount of wetting agent solution withdrawn is replaced with fresh wetting agent solution.

United States Patent Stein et al.

[ Mar. 11, 1975 CONTINUOUS PROCESS FOR THE Primary Examiner-Lewis GottsSEPARATION OF MIXTURES OF FATTY Assistant E.\'mniner-Ethel C. LoveSUBSTANCES OF DIFFERENT MELTING Attorney, Agent, or FirmHammond &Littell POINTS 57] ABSTRACT [75] Inventors: Werner Stein,Erkrath-Unterbach1 I f h k v Helmut Hartman, Langenfeld e lI'IVCHUOn reates to an improvement 0 t e noun both of Germany continuous process forthe separation of mlxtures of fatty substances of different meltingpoints. in which Asslgnee? Henkel & Cle GmbH, the starting mixture bytreating with an aqueous wet- Dusseldol'f-Hollhausen, Germany ting agentsolution is converted to a dispersion of liq- [22] Filed: Oct 26, 1972uid fatty substances and solid fatty substance particles. the formeddispersion IS separated into two phases of PP 300,895 different specificgravities, the lighter phase consists substantially of the liquid fattyfraction and the [30] Foreign Application Priority Data heav er phase ofa dispersion of the solid fatty parti- H 1971 Ge n 2155988 cles m theaqueous wetting agent SOlUllOl'l. After separma y ration of thissuspension the wetting agent solution 15 returned to the process. Theimprovement consists in [52} 260/419 260/420 1 3x withdrawing a part ofthe recycling wetting agent solution from said dispersion particles inthe aque- [5 re d of Search ous wetting agent Solution by Separation ofsome or a the aqueous solution from the solid fatty particles, the [56]References cued solid fatty particles containing adhering aqueous phaseUNITED STATES PATENTS and wetting agent are melted in the presence of an2.645.652 l/l953 Pramuk et al. 260/419 aqueous phase and the moltenfatty fraction contain- 2,800. 3 7/ 957 t in t a l 260/419 ing littlewetting agent, is separated from the aqueous $453545 7/1969 Faur ct260/419 phase enriched with wetting agent which is recycled g et and theamount of wetting agent solution withdrawn is HI mann e 'd 3.7374446/1973 Hartmann et al 260/4l9 replaced fresh Wemng agent 801mm 11Claims, 2 Drawing Figures PATENTEDHARI 1191s I ,735

sum 1 mi 2 F c; .1 :22 :0 I

l4 l6 j 1 CONTINUOUS PROCESS FOR THE SEPARATION OF MIXTURES OF FATTYSUBSTANCES OF DIFFERENT MELTING POINTS THE PRIOR ART German Patent No.977,544 discloses a process for the separation of mixtures of fatty acidesters, especially of triglyceride mixtures, into components ofdifferent melting points. This process involves preparing a dispersionof liquid fatty esters and separated solid fatty ester particles in anaqueous solution containing wetting agents and, optionally,non-surface-active electrolytes, and separating this dispersion into twophases of different specific gravities of which one consistssubstantially of the liquid fatty acid esters and the other of asuspension of the solid fatty acid esters in the aqueous wetting agentsolution. Solid jacket centrifuges have proved satisfactory for thisstep in the process. The solid fatty ester particles and the aqueouswetting agent solution are then separated in a known manner, e.g., byfiltration or by melting of the until then solid fatty acid esters, sothat the latter as a continuous liquid phase can be separated from theaqueous phase. The aqueous wetting agent solution, free of fatty acidesters, is then recycled in the process.

U.S. Pat. No. 2,800,493 discloses, in addition to this process for theseparation of mixtures of fatty acid esters, also a correspondingprocess for the separation of fatty acid mixtures into ingredients ofdifferent melting points. US. Pat. No. 2,972,636 describes theapplication of this process to mixtures of fatty alcohols. Thisseparation principle has become known under the name HydrophilizationProcess.

Improvements in this Hydrophilization Process are described incopending, commonly-assigned U.S. Pat. Application S.N. 102,471, filedDec. 29, 1970, now U.S. Pat. No. 3,737,444, and S.N. 102,712, filed Dec.30, 1970, now U.S. Pat. No. 3,733,343. According to these disclosures, apart of the wetting agent solution circulated during the separation offatty acid or fatty acid ester mixtures into components of differentmelting point by means of the Hydrophilization Process" is withdrawn andreplaced by fresh water, fresh electrolyte solution or fresh aqueouswetting agent solution in order to maintain the wetting agentconcentration essentially constant at the first separation step. Thisprocess is of special importance in the treatment of fatty acid mixtureswhich contain 0.8 percent to 15 percent by weight, preferably 1 percentto percent by weight of non-fatty acid organic impurities.

The term non-fatty acid organic impurities (in short NF) is to beunderstood to be organic substances which are derived from the rawmaterial serving for the preparation of the mixtures of fatty acids orfrom the processing of the mixtures of fatty acids, to be separated.These organic substances are those whose com position does notcorrespond to the formula RCOOH where R is a hydrocarbon containing 7 to27, preferably 9 to 21 carbon atoms, straight or branched aliphatic,optionally cycloaliphatic, saturated or unsaturated. Such NF contentsare found especially in undistilled fatty acids from a cleavage of thecorresponding fat.

Under organic impurities" or NF in the sense of the above definition areto be understood, among others, the substances occurring in naturalfats, which in the cleavage or saponification of these fats do notfurnish fatty acids but remain in the fatty acid mixtures. In addition,in fatty acids of synthetic origin, the organic impurities include theunreacted starting materials for the preparation of these fatty acids,such as paraffins, olefins, alcohols, aldehydes, etc., which, after theoptional working up of the crude fatty acids, remain partially orcompletely in the products of the process. These organic impurities maybe acidic, ester-like or unsaponified products, such as hydroxyfattyacids, fatty acid peroxides, fatty acid hydroperoxides, dicarboxylicacids (such as dimeric fatty acids) partial glycerides, fatty acid orhydroxyfatty acid esters of hydroxyfatty acids, alcohols, aldehydes,ketones, phosphatides, sterols, carotinoids, tocopherol, gossypol andother phenolic components, hydrocarbons, as well as decompositionproducts of the above-mentioned substances. Some of these organicimpurities may be separated from the fatty acids by distillation. Othershave about the same boiling range as the fatty acids so that apurification of the fatty acid mixtures by distillation only .is notalways possible. The amount of these impurities can be determined byknown analytical procedures. To I be sure, the decision if a certainstarting material has to be processed according to the process of theinvention, does not always require the preceding analyticaldetermination of all these above-mentioned NF components. It is mostlysufficient for the practice of the invention to determine the amounts ofnonsaponifiable material (US) and the amounts of partial ortri-glycerides. If the sum of these two NF components does not greatlyexceed the above minimum amounts, the determination of the other NFcomponents is not required.

It has already been suggested to add organic solvents to the fatty acidmixture to be separated with the aid of the hydrophilization process, inorder to attain in this way, in the crystallization of the solidingredients, an improvement of the separation effect. These organicsolvents are in the spirit of the invention not to be considered asimpurities derived from the preparation or the processing of the fattyacids.

The withdrawal from the recycling of wetting agent solution improves theseparating effect not only for fatty acid mixtures, but also in the caseof other fatty mixtures, especially when these faty mixtures containimpurities which adversely affect the dispersion and therefore theseparation result.

Provided the fractions of fatty substances obtained in thehydrophilization process are not chemically homogenous compounds, butare present as mixtures of components with different melting points,these fractions can be separated again in one or more further separationstages in the described manner. Thus, for example, the liquid phaseobtained could be cooled further to a temperature at which the highermelting components separate in crystalline form, and from this mixture,after dispersion in wetting agent solution, the higher and lower meltingfractions could again be isolated in the described way. It is therebypossible, but by no means necessary, to withdraw wetting agent solutionin each stage of separation and replace by fresh aqueous phase. It isoften sufficient to remove wetting agent solution only in one stage ofseparation. However, by these processes, even if the separation can beimproved by withdrawing wetting agent solution, a loss of wetting agentmust be taken into account.

OBJECTS OF THE INVENTION An object of the present invention is thedevelopment of an improvement in the Rewetting or I-IydrophilizationProcess whereby better separation of the higher and lower melting pointmixtures of fatty components are obtained continuously over long periodsof time.

Another object of the present invention is the development of acontinuous process for the separation of mixtures of fatty componentsinto fatty component mixtures of different melting points by the stepsof continuously dispersing said mixture of fatty components consistingof an oily phase and a solid phase in a recycling aqueous wetting agentsolution at a temperature whereby a dispersion of liquid and solid fattyparticles is obtained, continuously separating said dispersion into twophases of different specific gravities, a lighter phase consistingsubstantially of liquid fatty fractions and a heavier phase consistingsubstantially of solid fatty particles dispersed in said aqueous wettingagent solution, continuously withdrawing said liquid fatty fractions,continuously separating said solid fatty particles from some or all ofsaid aqueous wetting agent solution, continuously withdrawing saidseparated aqueous wetting agent solution, continuously melting saidsolid fatty particles containing adhering aqueous phase and wettingagent, in an aqueous phase, continuously separating said molten fattyfraction containing little wetting agent from an aqueous phase enrichedwith wetting agent, continuously withdrawing said molten fatty fraction,continuously recycling said aqueous phase enriched with wetting agent tosaid dispersing step and continuously replacing said withdrawn part ofsaid recycling aqueous wetting agent solution with a fresh aqueoussolution whereby the concentration of said recycling aqueous wettingagent solution is maintained substantially constant at said dispersingstep.

These and other objects of the present invention will become moreapparent as the description thereof proceeds.

THE DRAWINGS FIG. 1 is a flow diagram of the process of the invention.

FIG. 2 is a flow diagram of another embodiment of the process of theinvention.

DESCRIPTION OF THE INVENTION The above objects have been achieved by animproved process for the separation of fatty mixtures into components ofdifferent melting point by converting the fatty mixtures into adispersion of liquid and solid particles, separated from one another, ofthe fatty mixture in aqueous wetting agent solution, separation of thisdispersion into two phases of different specific gravities, the lighterof which consists substantially of the liquid fat fractions and theheavier consists of a suspension of the solid fat particles in aqueouswetting agent solution, isolation of the solid fat fractions from theaqueous wetting agent solution, when at least a part of the aqueouswetting agent solution is withdrawn and replaced by water or by aqueoussolution containing wetting agent and/or electrolyte, and the wettingagent which is not removed is returned to the process.

The process according to the invention is characterized in that theamount of wetting agent solution is removed from the said suspension,the solid fat particles are melted in the presence of the aqueous phase,the thereby formed, molten fat fraction reduced in wetting agent isseparated from the aqueous phase enriched with wetting agent and thelatter is returned to the process.

The particular advantage of this variation of the process lies in areduction of the losses of wetting agent which previously occurred. Theamounts of wetting agent contained in the solid fats are withdrawn whenthe solid fatty particles are separated during the cycle of the process,and the loss of wetting agent thereby caused would have to becompensated by addition of wetting agent. Surprisingly, small amounts ofwater are always sufficient to take up within the short time during themelting of the solid fatty particles the amounts of wetting agentcontained therein. The aqueous wetting agent solution thereby resultingis of a concentration such that it can profitably be taken back into theprocess. Owing to this, the losses of wetting agent fall considerably.

The fatty mixtures to be treated according to the invention include awide variety of fatty acid esters of vegetable, animal or syntheticorigin.

Examples of the fatty acid esters of vegetable origin are coconut fat orpalm kernel fat, palm oil, cottonseed oil, olive oil, soybean oil,peanut oil, linseed oil, rapeseed oil, castor oil, etc. Mixed fatty acidesters of animal origin are, for example, butter fat, chicken fat orgoose fat, lard, mutton tallow or beef tallow, suet and bone fats, andalso a large number of various fish fats and oils, train oil, blubber,whale oil, as for example menhaden oil, herring oil or sperm oil, codliver oil, etc. These fatty acid ester mixtures of natural origin aremostly triglycerides, but the invention is not limited to the separationof triglycerides; thus for example, sperm oil contains in addition totriglycerides also fatty alcohol-fatty acid-esters. The fatty acidesters of other alcohols are also useful as starting mixtures.

Besides the native triglycerides, further processed products of naturalfats can be separated, as for example, partly or completely hydrogenatedfats, interesterification products of natural fats or esterificationproducts of fatty acids and alcohols, as well as, very generally,derivatives of fatty acids and/or fatty alcohols of natural or syntheticorigin.

Furthermore, fatty acid mixtures are utilizable as starting materials tobe processed according to the invention which, for example, areobtainable by cleaving or by saponifying and acidifying fatty acidesters to the free fatty acids, especially from the fats occurring innature. The separation of the fatty acid mixtures obtainable from thevarious kinds of tallow into commercial stearic acid (sometimes calledstearin) and commercial oleic acid (sometimes called olein) are ofspecial practical importance. But synthetically prepared fatty acidsalso can be treated according to the invention.

Finally, mixtures of fatty alcohols may be separated which areobtainable by hydrogenation of fatty acids or fatty acid esters, whilethese fatty acids may be derived, for example, from the above-mentionednatural fats. Fatty alcohols prepared from synthetic fatty acids ortheir esters or directly occurring fatty alcohols of synthetic origin,however, can also be treated as starting materials.

The fatty residues present in the starting mixtures to be treatedaccording to the invention in the form of fatty acids or fatty alcoholspreferably contain 6 to 26, especially 8 to 20 carbon atoms. Whenpresent as esters, the fatty acid or fatty alcohol components preferablycontain the above amount of carbon atoms. According to the invention,compounds with branched chain fatty residues as well as resin ornaphthenic acids, their esters and corresponding alcohols also comeunder the term fatty substances.

As a matter of simplification, in the following specification themixture to be separated, of fatty components of different melting pointsis called starting material," the liquid phase obtained in theseparation is called oil, the solid phase obtained in the separation iscalled solid ingredients. The term solid ingredients is used for thehigher melting fatty particles even when they are present under the thenprevailing process conditions in a liquid state. The dispersion of solidand liquid fatty particles, to be separated from one another, in anaqueous wetting agent solution is denoted as dispersion" for the sake ofsimplicity and the suspension of solid fat particles in aqueous wettingagent solution coming from the centrifuge is denoted as suspension.

For the preparation of the dispersion of separated particles of solidfractions and oil, in aqueous wetting agent solution, a pasty mixture ofcrystalline solid fractions and oil is utilized. The separationobtainable according to the process is dependent, among other things, onthe quality of the solid crystals. In order to obtain a good separation,it is advisable to completely melt the starting mixture and then togradually cool it to the temperature at which the separation is to beeffected. Scraper coolers have proved suitable for cooling the moltenstarting mixture. These consist of tubes with a cooling jacket, whoseinner surface is kept free from the crystallizing solid fractions byrotating doctor blades. According to the crystallizing behavior of thestarting mixture, this can leave the scraper cooler in a more or lessstrongly supercooled liquid state. It is, therefore, advisable to givethe supercooled liquid starting mixture more time for crystallization ofthe higher melting solid ingredients before its further treatment.

The molten starting mixture, however, may also be cooled in another wayto the separating temperature, for example, by mixing it with water orwith aqueous wetting agent solution, and producing cold by evaporationof the water under reduced pressure. It is also possible to bring astarting mixture which has been precooled in the scraper cooler or byevaporation cooling, but is not yet at separation temperature to theseparation temperature, by mixing with a colder aqueous phase.

The wetting agent solution serving for the dispersion of the startingmixture cooled to the separating temperature frequently has the sametemperature as the mixture to be separated. The amount of the wettingagent solution should be about 0.5 to 3, preferably 1 to 2 parts byweight per part of the starting mixture to be separated present in thedispersion.

In addition to soaps, anionic or nonionic watersoluble compounds whichlower the surface tension of the aqueous solutions are utilizable. Aremoval of the liquid ingredients of the starting mixture from thesurface of the solid ingredients occurs with the aid of the aqueouswetting agent solution. The following compounds which contain an alkylradical with 8 to 18, preferably 10 to 16 carbon atoms in the moleculeare ammonium, mono-, dior triethanolammonium salts.

The water-soluble adducts of ethylene oxide to alkylphenols or fattyalcohols are useable as nonionic com pounds.

Appropriately, such amounts of wetting agents are used that in thedispersion formed, immediately prior to the entry in the separationcentrifuge, 0.05 to 2, preferably 0.1 to 1, parts by weight of wettingagent per parts by weight of aqueous solution are present.

' The above amounts for the wetting agents include not only the wettingagents actually dissolved in the aque ous phase, but also the amounts ofwetting agent dissolved in the oil or adsorbed on the surface of thesolid ingredients.

The effect of the aqueous wetting agent solution is improved if itcontains dissolved non-surface-active electrolytes, inert to thestarting mixtures. To this be long, e.g., the water-soluble chlorides,sulfates, or nitrates of monoto trivalent metals, particularly of thealkali, alkaline earth and earth metals. Above all, additions of sodiumsulfate and magnesium sulfate have proven desirable. The electrolyteconcentration of the dispersion to be separated, lies in the range of0.1 percent to 10 percent, preferably l percent to 5 percent, by weight.These numerical data, as also above in the case of the wetting agentconcentration, are calculated on the total amount of electrolytespresent in the dispersion based, however, on the aqueous phase presentin the dispersion. In connection with the invention, by aqueous wettingagent solution, preferably a wetting agent solution containingelectrolytes is meant.

In the mixing of the cooled starting mixture with the wetting agentsolution, the oil is displaced from the surfaces of the solidingredients, independently of whether the wetting agent solution ismixed with the starting mixture cooled to the separation temperature orwhether the liquid starting mixture together with the wetting agentsolution is brought to the separation temperature, so that the solidfractions are formed in the presence of the wetting agent solution. Ithas been found appropriate to combine the cooled starting mixture firstwith only a partial amount of a correspondingly more concentratedwetting agent solution, and to bring the so-formed more concentratedaqueous wetting agent solution gradually by addition of water,electrolyte solution, or correspondingly more dilute wetting agentsolution to the desired final concentration. Advantageously, the cooledstarting mixture is first combined with 5 percent to 50 percent,preferably 10 percent to 30 percent, of the total wetting agent solutionto be used, and gradually so much of further solution is added that thedesired final concentration is attained.

The dispersion is then separated into two phases of different specificgravity. Solid jacket centrifuges have,

proved specially advantageous for this purpose, and a number ofdifferent designs may be used, such as, for example, tube centrifuges,disk centrifuges, or continuous scaling centrifuges.

Of the phases thereby produced, the lighter or oil phase consistssubstantially of the liquid components of the starting mixture, and theheavier phase represents a suspension of the solids in aqueous wettingagent solution.

The wetting agent solution is now partly or completely removed from thissuspension according to the invention. By complete removal of thewetting agent solution is meant an operation in which the wetting agentsolution is separated until only amounts of liquid mechanically adheringto the solids are left, so that the solids are no longer obtained in aflowable state, but are obtained for example as a wet filter residue.Then an aqueous phase, for example, water or electrolyte solution, isadded in such amount that the solids again become flowable and may beadded as a liquid to the next stage of the process. The flowable aqueousslurry of the solids suitably contains 30 percent to 90 percent byweight, preferably 40 percent to 70 percent by weight of aqueous phase.

For the complete or partial separation of the wetting agent solutionfrom the suspension, filters, screen centrifuges, settling tanks, solidjacket centrifuges, hydrocyclones, centrifugal mud-separators andcentrifugal concentrators are suitable. In the preferred method ofoperation only about percent to 70 percent, preferably percent to 50percent of the wetting agent solution is removed, this amount beingadvantageously chosen as a function of the amount of water present inthe dispersion so that the solids are obtained as a still flowableconcentrate. The wetting agent solution can be removed continuously orportionwise from the suspension.

The remaining, still wet, solids preferably present as a flowableconcentrate are now heated to melt the solids. Two liquid phases areformed which are separated from one another in known way, for example,by separators or centrifuges. The aqueous phase thus obtained containsin solution a large part of the wetting agent contained in the solidfractions, and it is returned to the process. In this way, the wettingagent solution removed from the suspension can be replaced by freshsolution with a minimum loss of wetting agent. If necessary, the solidsmay be again washed with water in order to remove therefrom the lasttraces of wetting agent.

The process according to the invention is frequently carried out inseveral stages, in which one or both of the fractions obtained in thefirst separation stage is, or are, converted again into a dispersion ofsolid and liquid fatty components, separated from one another, ofcorrespondingly higher or correspondingly lower temperature, and theseare again separated. The process according to the invention can also beused for these further separation stages. When the solids obtained asintermediate fractions are returned to the process, it is oftensufficient to restrict the use of the variant of the process of theinvention to those end stages in which the solids are removed from theprocess as end products.

In FIG. 1, aflow diagram suitable for the execution of the separationprocess, according to the invention, is illustrated. The meltingstarting mixture, to be separated, is conducted through the feed pump 1to the scraping condenser 2, and leaves it as a pasty mixture of oil andsolid ingredients. This mixture passes into the mixer 3 which,advantageously, consist of several mixcooled starting material isstirred up with the more concentrated wetting agent solution, flowing inthrough the line 4, to give a dispersion. In the successive mixingchambers, the more dilute wetting agent or electrolyte solution isintermixed. Thereby, a dispersion is formed in which the oil particlesand the particles of the solid ingredients are separately dispersed inthe wetting agent solution. In order to convert the pasty startingmixture into a dispersion in aqueous wetting agent solution, however,other mixing devices are also suitable. It is sometimes sufficient toexpose the materials to be mixed to a turbulent flow.

This dispersion from the mixer 3 is then separated with the aid of asolid-jacket centrifuge 5 into an oil as the lighter phase and adispersion of the solid particles in the wetting agent solution as theheavier phase. The oily lighter phase is withdrawn by line 6. Theheavier phase is conducted through line 7, according to the invention tothe concentrator 26 where a part of the wetting agent solution isremoved and is discharged through line 15.

The feed pump 8 carries the remaining concentrated suspension of thesolids, possibly after addition of fresh aqueous phase, to the heater 9where the suspension is heated to melt the solid ingredients. Thewetting agent adhering to the solid fractions goes over into the aque'ous phase. The molten solid ingredients and the wetting agent solutionmove then together to the separator 10 from which the molten solidingredients leave at line 11 as the lighter phase and the wetting agentsolution leaves at line 12 as the heavier phase. This heavier aqueousphase containing the recovered wetting agent from the solid fraction isrecycled through the heat exchanger 13, through the line 14 to the mixer3.

In contrast to the methods of operation described in the examples of theabove-mentioned earlier applica tions, the wetting agent solutionwithdrawn according to the present invention, is thus removed before thesolids are melted. The wetting agent solution may be removedcontinuously or portionwise from time to time as required.

If the amount of aqueous phase removed in the concentrator 26 before themelting of the solids is not, or not completely, replaced by freshaqueous phase, a corresponding amount of fresh aqueous phase may beadded through line 16. It is, however, not absolutely necessary tointroduce the fresh solution where in FIG. 1, the line 16 dischargesinto the line 12 coming from the separator 10. Naturally, the freshsolution can be charged directly as wetting agent or electrolytesolution into the mixer 3, particularly into the successively arrangedmixing chambers designed for the dilution of the first formeddispersion.

According to a further embodiment of the invention, each of the twoobtained fatty fractions, the lower melting (oil) and/or the highermelting (solid ingredients) can be converted to a dispersion ofseparated solid fatty particles and liquid oil in aqueous wetting agentsolution, and from this a lower melting and a higher melting fattyfraction can be isolated. In addition, in these final separation stages,this variant of the-process according to the invention can be conductiveto a more complete recovery of the wetting agent.

If the oil, obtained in a preceding separation, is processed accordingto the invention procedure, it is cooled by one of the above-describedmethods, i.e., in the absence or also the presence of aqueous wettingagent solution, in comparison to the first separation step, to asuitably lower separation step, to a suitably lower separationtemperature (cold step). The wetting agent solution circulating in thesecond separation step can form its own wetting agent solution cycleseparated from that of the first separation step. The wetting agentsolution may, however, also flow through both separation steps.

If the process is applied at correspondingly higher temperatures to thesolid ingredients obtained in a preceding separation step (warm step),it can be carried out according to two process variants. The one variantconsists in heating the wetting agent solution with the dispersed solidingredients in it so that a part of the solid ingredients melts and nowforms an oil in this dispersion. The second variant consists incompletely melting the solid ingredients and to convert them again, asdescribed above, to a dispersion of separated particles of oil and solidparticles, from which the oil and the solid ingredients are isolated,however, at a higher temperature than was the case in the firstseparation step.

In FIG. 2 a flow diagram forthe renewed separation, at higher and lowertemperatures, of both fractions obtained in the first separation step isillustrated. The starting mixture, to be separated, is pumped by thepump 1 through the scraping condenser 2 into the mixer 3. This ispreferably constructed in the manner described above. It consists ofsingle mixing chambers through which the starting mixture issuccessively passed. In the first mixing chamber, the starting mixtureleaving the cooling and crystallizing scraping condenser 2 is firstcombined with more concentrated wetting agent solution through line 4.Water free of wetting agent, or electrolyte solution free of wettingagent, can be added through line 17, and wetting agent solutionrecovered from the solid fractions and recycled, is added through line14. The dispersion formed in the mixer 3 flows into the centrifuge 5 andis there separated into two phases. The heavier phase, present as asuspension of solid ingredients in aqueous wetting agent solution isdischarged through the line 7 into the concentrator 38. The separatedpart of the aqueous phase is removed at line 39. The remaining moreconeentrated suspension runs into the pump 8, while the lighter phaseconsisting substantially of oil is discharged through the line 6 forfurther treatment.

For the separation of small amounts of higher melting ingredients (coldstep) still present in this oil, it is conducted through the line 6 intothe mixer 3a. The latter may only consist of a simple mixing vessel. Inthe mixer 30, the oil is admixed with the wetting agent solution,returned from the process through line 20. If desired, through the lines19 or 21 more concentrated wetting agent solution and/or water, free ofwetting agent, or electrolyte solution, free of wetting agent, may beapplied. The aqueous solutions added at this point may have lowertemperatures than the oil. For this purpose, the recycling aqueouswetting agent solution can be cooled through the heat exchanger 13a. Theamount of this aqueous wetting agent solution is measured out by thevalve 29.

The dispersion formed in the mixer 3a, in which certain amounts ofcrystallized solid ingredients may already be present, is passed throughthe line 22 and the pump 18 into the scraping condenser 2a where it iscooled to the separation temperature. From there it is passed to thecentrifuge 5a from which an oil is withdrawn at line 23 as the lighterphase whose turbidity point is lower than the turbidity point of the oilleaving the centrifuge 5. At line 24, a suspension of solid ingredientsin aqueous wetting agent solution is obtained as the heavier phase whichis separated in the concentrator 26, and a part of the aqueous phase iswithdrawn through line 15. The pump 25 conveys the concentratedsuspension to the heater 9a which it leaves as a mixture of aqueouswetting agent solution and molten solid ingredients. In the separator 10this mixture is separated into the molten solid ingredient withdrawn atline 11 and the aqueous wetting agent solution withdrawn at line 12. Asubstantial part of the wetting agent adhering to the solid fraction ispresent in this aqueous wetting agent solution.

There are two possibilities for the processing at elevated temperatures(warm step) of the suspension of solid ingredients in aqueous wettingagent solution leaving the centrifuge 5: (a) either the total dispersionis heated to a temperature where a part of the solid ingredients melts,or (b) the suspension is heated to the complete melting of the solidingredients and then cooled to the separating temperature of the warmstep. In the first case, the pump 8 feeds the suspension, with valve 30closed, through the open valve 31 to a combi nation heating and coolingapparatus 32, which is heated in this case and from which then adispersion of oil and separated solid particles in aqueous wetting agentsolution leaves. In the second case, the pump 8 feeds the suspension,with the valve 31 closed, through the open valve 30 to the heatexchanger 9 where the solid ingredients are completly melted. Theemerging mixture is converted in the successively connected combinationheating and cooling and crystallizing apparatus 32 to a dispersion ofseparated particles of oil and solid ingredients in aqueous wettingagent solution. Either of these dispersions are separated in thecentrifuge 5b into the oil, withdrawn as the lighter phase at line 33,and the suspension of solid ingredients in aqueous wetting agentsolution, withdrawn as the heavier phase at line 34.

The suspension emerging at line 34 is concentrated in the concentrator41 by withdrawal of a part of the wetting agent solution emerging atline 42. The pump 35 feeds this concentrated suspension into the heater9b. The mixture of wetting agent solution and molten solid ingredientsformed is separated in the separator 10a into the molten solidingredients withdrawn at line 36 and into the aqueous wetting agentsolution. The latter is withdrawn at line 37.

The part of the warm concentrated wetting agent solution leaving theseparators l0 and 10a not withdrawn from circulation through lines 15and 42, is returned together to the process through the pump 27 and theline 40, and is cooled by passage through the heat exchanger 13 to thetemperature at which it shall enter into the first step. The valves 28and 29 control the partial amounts of recycling aqueous wetting agentsolution which are returned to the first or the cold step.

By the process scheme, according to FIG. 2, four fractions of differentmelting points or turbidity points are obtained. If tallow fatty acidsare separated in this manner into stearin and olein, the olein recoveredfrom the cold step and the stearin recovered from the warm step are theproper products of the process. The two other fractions of fatty acidsare returned to the starting material to be processed in the firstseparation step.

The following examples are illustrative of the process of the inventionwithout being deemed limitative in any respect.

EXAMPLES The fatty acids, the treatment of which is described in someExamples, were prepared from triglycerides by cleaving with water atelevated temperatures and increased pressure and then separating theaqueous glycerine-containing phase. Distillate fatty acids refer todistillates of these fatty acids as cleaved from triglycerides.

In Examples 1 to 6, starting materials were processed according to theflow diagram of FIG. 1. The molten starting mixture was passed throughthe pump 1 to the scraper cooler 2 and left this as a slurry of oil andsolid fractions. This slurry went to the mixer 3 consisting of severalmixing chambers in series, each provided with a stirrer. In the firstmixing chamber the cooled starting material was stirred with the wettingagent concentrate flowing through line 4 to give a dispersion. Thefollowing mixing chambers served for the dilution with wetting agentsolution or electrolyte solution. Provided it is not expressly statedotherwise, these solutions had the same temperature as the slurry of oiland solids emerging from the scraper cooler 2. In the mixer 3 thedispersion was formed, in which the oil particles and the solid fractionparticles, separated from one another, were present dispersed in thewetting agent solution (the data contained in the examples on thewetting agent and/or electrolyte contents also applies to thisdispersion. It includes the total amounts of wetting agent and/orelectrolyte present therein, but related to the aqueous phase).

The solid jacket centrifuge 5 separated this dispersion into the lighteroil obtained at line 6 and the heavy suspension obtained at line 7. Thelatter was separated in the concentrator 26 (a centrifugal separatorserved for this purpose) into a concentrated suspension and a weaksolution of wetting agent free from solid fractions. This solution wasdiscarded through line 15. The concentrated suspension was passed bymeans of the pump 8 to the heater 9, where the suspension was heateduntil the solids melted. The wetting agent adhering to the solidfractions thereby went over for the most part into the residual aqueousphase. Molten solids and wetting agent solution then passed together tothe separator 10, from which the molten solids emerged as the lighterphase at line 11, and the wetting agent solution as the heavier phaseemerged at line 12. This heavier phase with the recovered wetting agentcontained therein went through the heat exchanger 13 and the line 14back into the mixer 3. The loss of liquid emerging at line 15 by theremoval of wetting agent solution was compensated by addition of freshaqueous phase at line 16.

It is not absolutely necessary to introduce the fresh solution at theplace where in the drawing the line 16 feeds into line 12. The freshsolution can obviously also be fed directly into the mixer 3, especiallyinto the final mixing vessels intended for the dilution of the firstformed dispersion.

Although the higher melting fractions obtained are present in the moltenstate, they are for the sake of simplicity referred to as solidfractions."

In the Examples the consumption of wetting agent in the processaccording to the invention is co pared with the consumption of wettingagent in operation without withdrawing recycling wetting agent solutionor with withdrawing of wetting agent solution after melting theseparated solid fractions. The separation process without withdrawing apart of the recycling wetting agent solution is indeed known inprinciple. but the details of the conditions used in the process comefrom internal unpublished work. Therefore, these comparative examplesare not to be regarded as the state of the art. In the method describedfor comparison relating to withdrawal of part of the wetting agentsolution after melting the solid fractions the concentrator 26 wasavoided by a conduit leading from the line 7 direct to the pump 8. Thewetting agent solution was removed in line 12 by a discharge cock. Thebypass conduit and the discharge cock are not shown in FIG. 1. This typeof withdrawal of part of the recycling wetting agent solution is theobject of the earlier US. Pat. Applications Ser. Nos. 102,471 and102,712.

The NF contents (NF non-fatty acid-like components) indicated in theExamples of the fatty acid mixtures to be separated are the sums of theunsaponifiable contents and the glyceride contents. The latter arecalculated from the analytically determined contents of ester-like boundglycerine with the calculated presumption that all glycerine is presentas diglyceride ac tually: mixture of mono-, diand tri-glycerides) andthat the fatty acids present in the glycerides have the same averagemolecular weight as the free fatty acids.

EXAMPLE 1 a. Treatment of distilled fatty acid cleaved from tallow (AcidN0. 204, Saponification N0. 206, Iodine N0. 52, NF 1 percent byweight) 1. Conventional operation without withdrawal of wetting agentsolution:

I t/h (1,000 kg/h) of this starting mixture was cooled in the scrapingcondenser to 5C. The pasty mix.- ture of oil and solid ingredientsobtained was first admixed with 0.3 t/h of more concentrated andsubsequently with 1.2 t/h of more dilute wetting agent solution, so thatthe dispersion leaving the mixer contained, per one part by weight ofthe cooled starting material, 1.5 part by weight of wetting agentsolution. This wetting agent solution had a wetting agent content of0.25 percent by weight of sodium decylsulfate and an electrolyte contentof I percent by weight of MgSO The dispersion was then separated into anoily and an aqueous phase. As oily phase, 0.39 t/h of olefin with aturbidity point of 4C were obtained. After process of the aqueous phase,0.61 t/h of stearin with an I. N0. 28 were obtained. The aqueous wettingagent solution was totally recycled.

2. Conventional operation with withdrawal of part of the recyclingwetting agent solution:

When the same fatty acid was treated in an analogous way, but withcontinuous withdrawal of 0.2 t/h of wetting agent solution from thecycle at a place (not shown) in the line 12 and replacement of theremoved amount by the same amount of 1% MgSO solution (at line 16) withat the same time introduction of an amount of more concentrated wettingagent solution (by line 4) such that the wet ting agent content of thedispersion remained permanently at the calculated value, 0.52 t/h ofstearin (1.NO. 17) and 0.48 t/h of olein (turbidity point 4C) wereobtained. Thus by the withdrawal of part of the recycling wetting agentsolution and its replacement, a purer stearin and a higher yield ofolein were obtained. Of course 2 kg of sodium dodecyclsulfate per r ofwithdrawn wetting agent solution were lost.

3. Operation according to the present invention:

But when 0.2 t/h of wetting agent solution were withdrawn from the cyclein the concentrator 26, i.e., from the cold suspension, the loss ofwetting agent was reduced by 65 percent to 0.7 kg/t of withdrawn wettingagent solution.

b. Treatment of undistilled fatty acid cleaved from tallow (Acid N0.199, Saponification N0. 206, 1 N0. 53, NF 4.5 percent by weight) 1.Conventional operation without withdrawal of wetting agent solution:

This starting material was treated essentially under the same conditionsas described in Example 10. The content of sodium decylsulfate in thedispersion was increased to 0.3 percent by weight. In spite of theincreased wetting agent content, the separation results wereunsatisfactory. After processing, 0.355 t/h of olein (turbidity point4C) and 0.645 t/h of stearin (I N0. 31) were obtained.

2. Conventional operation with withdrawal of wetting agent solution:

On the other hand, in a way similar to that described in Example 1a (2)with the same constant content of sodium decylsulfate, 0.5 t/h of thewetting agent solution was removed from the cycle and replaced by 0.5t/h of 1% MgSO solution, then 0.46 t/h of olein (turbidity point 4C) and0.54 t/h of stearin (I N0. 19) were obtained. However 2.5 kg of sodiumdodecylsulfate per t of withdrawn wetting agent solution were lost.

3. Operation according to the invention:

But when, as described above, the 0.5 t/h of wetting agent solution wasremoved at line 15, i.e., from the cold stearin suspension, the loss ofwetting agent was reduced by 68 percent to 0.8 kg/t of withdrawn wettingagent solution.

EXAMPLE 2 a. Treatment of distilled cottonseed oil fatty acids (Acid N0.202, Saponification N0. 204, I. N0. 103, NF=1.7 percent by weight).

1. Conventional operation without withdrawal of wetting agent solution:

Starting material cooled to 5C (separating temperature) Dispersionformed from 1 t/h of cooled fatty acids 0.4 t/h of more concentratedwetting agent solution, diluted with 1.3 t/h of recycled wetting agentsolution.

Composition of the wetting agent solution: 0.25 percent by weight ofsodium decylsulfate and 2 percent by weight of Na,so,.

Process products:

0.77 t/h of liquid fatty acids (turbidity point 6C, I

0.23 t/h of solid fatty acids (1 N0. 26)

2. Conventional operation with withdrawal of wetting agent solution:

Withdrawn wetting agent solution: 0.4 t/h replaced by Na SQ, solution,with the content of wetting agent and Na SQ, held constant.

Process products:

078 t/h of liquid fatty acids (turbidity point 6C, 1

0.22 t/h of solid fatty acids (l N0. 18)

Loss of wetting agent: 2.4 kg/t of withdrawn wetting agent solution.

3. Operation according to the invention:

The 0.4 t/h of wetting agent solution was removed by means ofahydrocyclone from the cold suspension. Owing to this the loss of wettingagent fell by 71 percent to 0.7 kg/t of withdrawn wetting agentsolution.

b. Treatment of undistilled fatty acid cleaved from cottonseed oil (AcidN0. 197, Saponification No. 204,1 N0. 103, NF 4.4 percent by weight) 1.Conventional operation without withdrawal of the wetting agentsolutions:

Starting material cooled to 5C (separating temperature) Dispersionformed from 1 t/h of cooled fatty acids, 04 t/h of more concentratedwetting agent solution diluted with 1.5 z/h of recycled wetting agentsolutlon.

Composition of the wetting agent solution: 0.45 percent by weight ofsodium decylsulfate and 2.5 percent by weight of Na SO Process products:

0.735 t/h of liquid fatty acids (turbidity point 3C,I

0.265 t/h of solid fatty acids (1 N0. 33)

2. Conventional operation with withdrawal of wetting agent solution:

Withdrawn wetting agent solution: 0.7 t/h replaced Na SO solution, withthe content of wetting agent and Na SO held constant.

Process products:

0.770 t/h of liquid fatty acids (turbidity point 3C, 1

0.230 t/h of solid fatty acids (1 N0. 21).

Loss of wetting agent: 2.6 kg/t of withdrawn wetting agent solution.

3. Operation according to the invention:

When 0.7 t/h of wetting agent solution was removed by means of acentrifuge from the cold suspension, the loss of wetting agent fell byabout 81 percent to 0.5 kg/t of withdrawn wetting agent solution.

EXAMPLE 3 Treatment of distilled fatty acid cleaved from fish oil (AcidN0. 199, Saponification N0. 201, I No.- 126, NF 1.8 percent byweight) 1. Conventional operation without withdrawal of the wettingagent solution:

Starting mixture cooled at 5C (separation temperature).

Dispersion formed from 1 t/y of cooled fatty acids, 0.5 t/h of moreconcentrated wetting agent solution diluted with 1.5 t/h of recycledwetting agent solution. Composition of the wetting agent solution: 0.3percent by weight of sodium decylsulfate and 2 percent by weight of MgSOProcess products 0.795 t/h of liquid fatty acids (turbidity point 3C, I

0.205 t/h of solid fatty acids (I N0. 34)

2. Conventional operation with withdrawal of the wetting agent solution:

Withdrawn wetting agent solution: 0.45 t/h replaced MgSO, solution withthe content of wetting agent and MgSO, held constant.

Process products 0.81 t/h of liquid fatty acids (turbidity point 3C, I

0.19 t/h of solid fatty acids (1 N0. 23).

Loss of wetting agent: 2.2 kg/t of withdrawn wetting agent solution.

3. Operation according to the invention:

When 0.45 t/h of wetting agent solution were removed from the coldsuspension the loss of wetting agent fell by about 68 percent to 0.7kg/t of withdrawn wetting agent solution.

EXAMPLE 4 .Treatment of distillation deacidified palm oil (Acid N0. 1.1,Saponification N0. 201, I N0. 49).

I. Conventional operation with withdrawal of the wetting agent solution:

Starting material cooled to 30C (separation temperature) Dispersionformed from 50 kg/h of cooled palm oil and 40 kg/h of wetting agentsolution. Composition of the wetting agent solution: 0.6 percent byweight of sodium dodecylsulfate and 5 percent by weight of Na SOWithdrawn wetting agent solution: I kg/h replaced y Na SO solution, withthe content of wetting agent and Na SO held constant. Process products:

45.5 kg/h of oil (rising melting point 31C, I N0.

5 3) 4.5 kg/h of solid fractions (rising melting point 52C,

I N0. 19.8) Loss of wetting agent: 5.5 g/kg of withdrawn wetting agentsolution.

2. Operation according to the invention: When kg/h of wetting agentsolution were removed from the cold suspension, the loss of wettingagent fell by 93 percent to 0.4 g/kg of withdrawn wetting agent solutionEXAMPLE 5 1. Conventional operation with withdrawal of wetting agentsolution:

Starting mixture: The lower melting fractions from palm oil (risingmelting point 31C, I N0. 53) ob- Withdrawn wetting agent solution: 10kg/h replaced by fresh wetting agent solution, with the content ofwetting agent and MgSO, held constant.

Process products:

38 kg/h of an oil, liquid at 20C (I N0. 58.5) 12 kg/h of solid fractions(I N0. 34, rising melting point 36C) with largely cacoa butter-likeproperties.

Loss of wetting agent: 5.9 g/kg of withdrawn wetting agent solution.

2. Operation according to the invention:

When 10 kg/h of wetting agent solution were re moved from the coldsuspension, the wetting agent consumption fellby 98 percent to 0.l g/kgof withdrawn wetting agent solution.

EXAMPLE 6 ondary alcohols with 14 to 15 carbon atoms, 5 percent byweight of Na SO Withdrawn wetting agent solution: 8 kg/h replaced by NaSO solution, with the content of wetting agent and Na SO held constant.

Process products:

kg/h of oil (Acid N0. 13.0, Saponification N0.

15 kg/h of solid fractions (Acid N0. 6.2, Saponification N0. 262, I N0.7.8, rising melting point 324C).

Loss of wetting agent: 4.6 g/kg of withdrawn wetting agent solution.

Operation according to the invention:

When 8 kg/h of wetting agent solution were removed from the coldsuspension, the loss of wetting agent fell by 93 percent to 0.3 g/kg ofwithdrawn wetting agent solution.

EXAMPLE 7 This example describes the processing of an undistilled fattyacid mixture (Acid N0. 204, Saponification N0. 207, I N0. 49, NF 0.9percent) obtained by the cleaving of beef tallow of technical quality,into olein and commercial stearin with use of an apparatus according toFIG. 2, whereby the fractions obtained in the first separation step wereseparated in one successively arranged step each (warm step or coldstep). Part of the wetting agent solution was withdrawn in each case. Inthe conventional operation this occurred after the hot or cold stage,i.e., the wetting agent solution was removed after melting the solidfractions downstream of the separators l0 and 10a by valves (not shown).The centrifuges 26, 38 and 41 operating as concentrators were avoided bylines which are not shown in FIG. 2 for reasons of good visibility. inthe operation according to the invention part of the wetting agentsolution was removed from the cold suspensions,

which emerge from the centrifuges 5, a and 5b, by the concentrators 26,38 and 41, the wetting agent solution emerging at lines 15, 39 and 42.The loss of wetting agent solution thereby occurring is compensated byaddition of fresh aqueous phase.

Conventional operation with withdrawal of the wetting agent solution:

The starting mixture was cooled to 30C with a throughput of 1 t/h in thescraping condenser 2 and admixed in the mixer 3 with 0.2 t/h of a 1% NaSO solution at 28C added at line 17, and 1.4 t/h of a 1% NaSO solutionat 29C, recycled from the process, containing sodium dodecylsulfateadded at line 14. In addition, such amounts of a percent sodiumdodecylsulfate solution were measure out and added at line 4, that thedispersion leaving the mixer 3 with a temper ature of 29C contained 0.19percent by weight of sodium dodecylsulfate, based on the aqueous phase.From the centrifuge 5, 604 kg/h of olein (I N0. 74) and an aqueousdispersion of 396 kg/h of a commercial stearin (I N0. 11) wereseparated.

This dispersion was led through the warm step with the aid of thefeeding pump 8, with the valve 30 closed, passed the valve 31 andthrough the scraping cooler 32, heated with hot water. A warm dispersionat 493C of oil and solid ingredients was formed which was separated inthe solid-jacket centrifuge 5b, maintained at 49 to 50C. At line 33, 72kg/h of a liquid fatty acid (I N0. 35) were obtained. The suspension ofthe solid ingredients in aqueous wetting agent solution was fed throughthe pump 35 to the heat exchanger 9b and then heated to 90C. From theseparator 10a at line 36, 324 kg/h of a commercial stearin (I N0. 6.1)were obtained.

The 604 kg/h of olein at 29C, obtained in the first separation step,were admixed in the mixer 3a with 500 kg/h of recycled sodiumdodecylsulfate solution containing l percent of Na SO at a temperatureof 16C added at line 20, and with as much of 10 percent sodiumdodecylsulfate solution added at the 21 that the sodium dodecylsulfatecontent of the formed dispersion, containing already certain amounts ofsolid ingredients, was 0.18 percent by weight, based on the aqueousphase. This dispersion was cooled in the scraping condenser 2a to 8C,and separated in the solid-jacket centrifuge 5a into 416 kg/h of olein(I N0. 90, turbidity point 6C) and into an aqueous suspension of 188kg/h of solid fatty acid (I N0. 38) in aqueous wetting agent solution.

The 416 kg/h of olein (I N0. 90) obtained in the cold step, and the 324kg/h of commercial stearin (I N0. 6) obtained in the warm step, areconsidered as final products, the intermediate fractions (188 kg/h offatty acids (1 N0. 38) solid at 8C, and the 72 kg/h of fatty acids (1N0. 35) liquid at 49C, were combined and returned to the process.

Of the wetting agent solution recycling at about 1.6 t/h, after theseparation of the molten solid fractions, about 0.6 t/h (37.5 percent)were withdrawn out and replaced.

The loss of wetting agent was 2.2 kg/t of withdrawn wetting agentsolution.

Operation according to the invention:

When 0.6 t/h of withdrawn wetting agent solution were removed from thecold solid dispersions (0.2 t/h each at lines 15, 39 and 42) the loss ofwetting agent fell in the remaining similar operation by 64 percent to0.8 kg/t of withdrawn wetting agent solution.

The preceding specific embodiments are illustrative of the practice ofthe invention. It is to be understood, however, that other proceduresknown to those skilled in the art may be employed without departing fromthe spirit of the invention or the scope of the appended claims.

We claim:

1. A continuous process for the separation of mixtures of fatty acidscontaining from 0.8 percent to 15 percent by weight of non'fatty acidorganic impurities into fatty acid mixtures of different melting pointsby the steps of continuously dispersing said mixture of fatty acidsconsisting of an oily phase and a solid phase in a recycling aqueouswetting agent solution at a tem perature whereby a dispersion of liquidand solid fatty acid particles is obtained, continuously separating saiddispersion into two phases of differentspecific gravities, a lighterphase consisting substantially of liquid fatty acid fractions and aheavier phase consisting substantially of solid fatty acid particlesdispersed in said aqueous wetting agent solution, continuouslywithdrawing said liquid fatty acid fractions, continuously separatingsaid solid fatty acid particles from 10 percent to percent by weight ofsaid aqueous wetting agent solution, continuously withdrawing saidseparated aqueous wetting agent, solution, continuously melting saidsolid fatty acid particles containing adhering aqueous phase and wettingagent, in an aqueous phase, continuously separating said melted fattyacid particles containing little wetting agent from an aqueous phaseenriched with wetting agent, continuously withdrawing said melted fattyacid particles, continuously recycling said aqueous phase enriched withwetting agent to said dispersing step and continuously replacing saidwithdrawn part of said recycling aqueous wetting agent solution with afresh aqueous solution whereby the concentration of said recyclingaqueous wetting agent solution is maintained substantially constant atsaid dispersing step.

2. The process of claim 1 wherein the amount of said separated aqueouswetting agent solution withdrawn is such that said solid fatty particlesare obtained in a concentrated aqueous suspension which is flowable.

3. The process of claim 1 wherein the amount of said separated aqueouswetting agent solution withdrawn is practically free to fatty particlesand is from 15 percent 0t 50 percent by weight of said recycling aqueouswetting agent solution.

4. The process of claim 1 wherein said separated aqueous wetting agentsolution withdrawn is approximately all that separated from said solidfatty particles and fresh aqueous phase is added to this separated solidfatty particles to form a flowable slurry.

5. The process of claim 1 wherein said solid fatty particles containingadhering aqueous phase and wetting agent in an aqueous phase containfrom 40 percent to 70 percent by weight of water.

6. The process of claim 4 wherein said solid fatty particles containingadhering aqueous phase and wetting agent in an aqueous phase containfrom 40 percent to 70 percent by weight of water.

7. The process of claim 1 wherein said mixture of fatty acids is aliquid fatty acid mixture previously separated by the process.

19 20 8. The process of claim 1 wherein said mixture of 10. The processof claim 1 wherein said mixtures of fatty acids is a solid fatty acidmixture previously sepafatty acids are undistilled cleaved triglyceridefatty rated by the process. acids.

9. The process of claim 1 wherein said mixture of 11. The process ofclaim 1 wherein said mixtures of fatty acids contains from 1 percent topercent by 5 fatty acids is cleaved tallow.

weight of said non-fatty acid organic impurities.

1. A continuous process for the separation of mixtures of fatty acidscontaining from 0.8 percent to 15 percent by weight of non-fatty acidorganic impurities into fatty acid mixtures of different melting pointsby the steps of continuously dispersing said mixture of fatty acidsconsisting of an oily phase and a solid phase in a recycling aqueouswetting agent solution at a temperature whereby a dispersion of liquidand solid fatty acid particles is obtained, continuously separating saiddispersion into two phases of different specific gravities, a lighterphase consisting substantially of liquid fatty acid fractions and aheavier phase consisting substantially of solid fatty acid particlesdispersed in said aqueous wetting agent solution, continuouslywithdrawing said liquid fatty acid fractions, continuously separatingsaid solid fatty acid particles from 10 percent to 70 percent by weightof said aqueous wetting agent solution, continuously withdrawing saidseparated aqueous wetting agent, solution, continuously melting saidsolid fatty acid particles containing adhering aqueous phase and wettingagent, in an aqueous phase, continuously separating said melted fattyacid particles containing little wetting agent from an aqueous phaseenriched with wetting agent, continuously withdrawing said melted fattyacid particles, continuously recycling said aqueous phase enriched withwetting agent to said dispersing step and continuously replacing saidwithdrawn part of said recycling aqueous wetting agent solution with afresh aqueous solution whereby the concentration of said recyclingaqueous wetting agent solution is maintained substantially constant atsaid dispersing step.
 1. A CONTINUOUS PROCESS FOR THE SEPARATION OFMIXTURES OF FATTY ACIDS CONTAINING FROM 0.8 PERCENT TO 15 PERCENT BYWEIGHT OF NON-FATTY ACID ORGANIC IMPURITIES INTO FATTY ACID MIXTURES OFDIFFERENT MELTING POINTS BY THE STEPS OF CONTINUOUSLY DISPERSING SAIDMIXTURE OF FATTY ACIDS CONSISTING OF AN OILY PHASE AND A SOLID PHASE INA RECYCLING AQUEOUS WETTING AGENT SOLUTION AT A TEMPERATURE WHEREBY ADISPERSION OF LIQUID AND SOLID FATTY ACID PARTICLES IS OBTAINED,CONTINUOUSLY SEPARATING SAID DISPERSION INTO TWO PHASES OF DIFFERENTSPECIFIC GRAVITIES, A LIGHTER PHASE CONSISTING SUBSTANTIALLY OF LIQUIDFATTY ACID FRACTIONS AND A HEAVIER PHASE CONSISTING SUBSTANTIALLY OFSOLID FATTY ACID PARTICLES DISPERSED IN SAID AQUEOUS WETTING AGENTSOLUTION, CONTINUOUSLY WITHDRAWING SIAD LIQUID FATTY ACID FRACTIONS,CONTINUOUSLY SEPARATING SAID SOLID FATTY ACID PARTICLES FROM 10 PERCENTTO 70 PERCENT BY WEIGHT OF SAID AQUEOUS WETTING AGENT SOLUTION,CONTINUOUSLY WITHDRAWING SAID SEPARATED AQUEOUS WETTING AGENT, SOLUTION,CONTINUOUSLY MELTING SAID SOLID FATTY ACID PARTICLES CONTAINING ADHERINGAQUEOUS PHASE AND WETTING AGENT, IN AN AQUEOUS PHASE, CONTINUOUSLYSEPARATING SAID MELTED FATTY ACID PARTICLES CONTAINING LITTLE WETTINGAGENT FROM AN AQUEOUS PHASE ENRICHED WITH WETTING AGEMT, CONTINUOUSLYWITHDRAWING SAID MELTED FATTY ACID PARTICLES, CONTINUOUSLY RECYCLINGSAID AQUEOUS PHASE ENRICHED WITH
 2. The process of claim 1 wherein theamount of said separated aqueous wetting agent solution withdrawn issuch that said solid fatty particles are obtained in a concentratedaqueous suspension which is flowable.
 3. The process of claim 1 whereinthe amount of said separated aqueous wetting agent solution withdrawn ispractically free to fatty particles and is from 15 percent ot 50 percentby weight of said recycling aqueous wetting agent solution.
 4. Theprocess of claim 1 wherein said separated aqueous wetting agent solutionwithdrawn is approximately all that separated from said solid fattyparticles and fresh aqueous phase is added to this separated solid fattyparticles to form a flowable slurry.
 5. The process of claim 1 whereinsaid solid fatty particles containing adhering aqueous phase and wettingagent in an aqueous phase contain from 40 percent to 70 percent byweight of water.
 6. The process of claim 4 wherein said solid fattyparticles containing adhering aqueous phase and wetting agent in anaqueous phase contain from 40 percent to 70 percent by weight of water.7. The process of claim 1 wherein said mixture of fatty acids is aliquid fatty acid mixture previously separated by the process.
 8. Theprocess of claim 1 wherein said mixture of fatty acids is a solid fattyacid mixture previously separated by the process.
 9. The process ofclaim 1 wherein said mixture of fatty acids contains from 1 percent to10 percent by weight of said non-fatty acid organic impurities.
 10. Theprocess of claim 1 wherein said mixtures of fatty acids are undistilledcleaved triglyceride fatty acids.